CN111533259B - Reaction partition adjustable two-stage anoxic/aerobic biological membrane sewage treatment system - Google Patents
Reaction partition adjustable two-stage anoxic/aerobic biological membrane sewage treatment system Download PDFInfo
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 40
- 239000010865 sewage Substances 0.000 title claims abstract description 39
- 238000005192 partition Methods 0.000 title claims abstract description 5
- 239000012528 membrane Substances 0.000 title claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 87
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 27
- 238000005273 aeration Methods 0.000 claims description 44
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 36
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 32
- 238000010992 reflux Methods 0.000 claims description 28
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims description 24
- 238000003756 stirring Methods 0.000 claims description 22
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 16
- 229910002651 NO3 Inorganic materials 0.000 claims description 14
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 13
- 239000005416 organic matter Substances 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 12
- 230000015556 catabolic process Effects 0.000 claims description 10
- 238000006731 degradation reaction Methods 0.000 claims description 10
- 230000001546 nitrifying effect Effects 0.000 claims description 10
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims description 8
- 239000000969 carrier Substances 0.000 claims description 6
- 230000033228 biological regulation Effects 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000010802 sludge Substances 0.000 description 10
- 230000001276 controlling effect Effects 0.000 description 8
- 239000000758 substrate Substances 0.000 description 6
- 239000013589 supplement Substances 0.000 description 6
- 230000032770 biofilm formation Effects 0.000 description 5
- 238000005352 clarification Methods 0.000 description 4
- 238000012258 culturing Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000006396 nitration reaction Methods 0.000 description 4
- 125000001477 organic nitrogen group Chemical group 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 206010021143 Hypoxia Diseases 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
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- 238000005188 flotation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
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- 235000017281 sodium acetate Nutrition 0.000 description 1
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- 239000000725 suspension Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
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Abstract
A reaction partition adjustable two-stage anoxic/aerobic biomembrane sewage treatment system is characterized in that: the device comprises a first-stage A/O unit and a second-stage A/O unit which are connected in sequence; the first-stage A/O unit comprises a first anoxic reactor, a second anoxic/aerobic reactor, a third aerobic reactor, a fourth aerobic reactor and a fifth aerobic reactor which are connected in sequence; the second-stage A/O unit comprises a sixth anoxic reactor, a seventh anoxic reactor and an eighth aerobic reactor which are connected in sequence. The system improves the high-efficiency utilization and denitrification efficiency of the carbon source in raw water by the arrangement of the front-mounted denitrification and the rear-mounted denitrification, realizes the effective control of the denitrification capability of the system according to the treatment target requirement by the accurate control of the addition of the exogenous carbon source in the rear-mounted denitrification, achieves the most economical and stable sewage denitrification treatment, is suitable for sewage treatment with high discharge standard, and can automatically control and adjust the reaction space and the reaction condition.
Description
Technical Field
The invention relates to a system for sewage treatment through an anoxic/aerobic biomembrane, belonging to the technical field of sewage treatment.
Background
With the improvement of the discharge standard of water pollutants of a sewage treatment plant, especially the stricter requirements on the water quality index related to nitrogen element, the traditional A taking activated sludge as the main component2the/O and the deformation process thereof obviously cannot meet the requirements, and in order to improve the denitrification efficiency of the urban sewage, a longer sludge age and a longer hydraulic retention time need to be set, and a higher aeration rate needs to be controlled, so that the high investment and the high energy consumption are in conflict with the green development mode advocated by the state.
The fluctuation of water quality, water quantity and water temperature directly influences the efficiency and stability of the sewage treatment system, and thus the construction investment and the operation cost of the sewage treatment project are high. Therefore, on the premise of ensuring that the high discharge standard is achieved, the reduction of the influence of water quality, water quantity and water temperature fluctuation and the investment of treatment engineering construction and the operation cost thereof become the key for improving the economy of urban sewage treatment.
Although the lack/aerobic process and the biomembrane technology are the prior art, the single-stage or multi-stage A/O process of the existing activated sludge method is that the activated sludge circularly runs and reacts under the alternate environment of oxygen deficiency and oxygen deficiency, and the activated sludge method system can not realize the partition functional design, and has low biological denitrification efficiency and high investment and running cost.
Therefore, an economical and efficient biological denitrification treatment technology for urban sewage is urgently needed.
Disclosure of Invention
Aiming at the technical requirements of efficient denitrification for urban sewage treatment and the aim of improving the economy of sewage treatment, the invention provides a two-stage anoxic/aerobic biomembrane sewage treatment system with adjustable reaction zones, and the optimal economy of sewage treatment under different seasonal changes is achieved by automatically controlling and adjusting the reaction space and the operation conditions.
The invention relates to a two-stage anoxic/aerobic biomembrane sewage treatment system with adjustable reaction zones, which adopts the following technical scheme.
The system comprises a first-stage A/O unit and a second-stage A/O unit which are connected in sequence; the first-stage A/O unit comprises a first anoxic reactor, a second anoxic/aerobic reactor, a third aerobic reactor, a fourth aerobic reactor and a fifth aerobic reactor which are connected in sequence; the second-stage A/O unit comprises a sixth anoxic reactor, a seventh anoxic reactor and an eighth aerobic reactor which are connected in sequence; suspended biological membrane carriers are filled in each reactor; stirring devices are arranged in the first anoxic reactor, the sixth anoxic reactor and the seventh anoxic reactor and in the second anoxic/aerobic reactor; aeration devices are arranged in the third aerobic reactor, the fourth aerobic reactor, the fifth aerobic reactor, the eighth aerobic reactor and the second anoxic/aerobic reactor.
The filling rate of the suspended biological membrane carrier is as follows: the filling rate in the first anoxic reactor, the sixth anoxic reactor and the seventh anoxic reactor is not more than 45 percent, the filling rate in the second anoxic/aerobic reactor and the fifth aerobic reactor is not more than 40 percent, and the filling rate in the third aerobic reactor, the fourth aerobic reactor and the eighth aerobic reactor is not more than 55 percent.
The stirring device adopts a spiral or hyperboloid stirrer, and the stirring input power is not less than 25W/m3。
The aeration device adopts a mode of arranging perforated pipes on one side for aeration, and the air flow of aeration orifices is 1.60-1.75 m3/h。
And an effluent suspended biofilm carrier intercepting screen is arranged in each reactor, the maximum sieving flow speed of the intercepting screen is not more than 60m/h, the aperture ratio of the intercepting screen is not more than 60%, and the aperture of the screen is 60% of the diameter of the suspended biofilm carrier.
The water inlet end of the first-stage A/O unit is provided with an online flow analyzer and an online COD analyzer; the water outlet end of the first anoxic reactor is provided with an online nitrate nitrogen analyzer; and the water outlet end of the fifth aerobic reactor is provided with an online ammonia nitrogen analyzer, an online nitrate nitrogen analyzer and an online dissolved oxygen analyzer.
The second anoxic/aerobic reactor is controlled and regulated according to the following processes:
when the second anoxic/aerobic reactor is in a state of stirring opening and aeration closing, the second anoxic/aerobic reactor is used as an anoxic denitrification reactor for denitrification; when the nitrogen concentration of nitrate in the effluent of the first anoxic reactor is lower than or equal to the set value C1And the holding time exceeds the set value T1When the second anoxic/aerobic reactor is used, the stirring is automatically closed, the aeration is started, namely the anoxic state is converted into the aerobic state, and the reactor is used as an aerobic reactor for organic matter degradation; when the nitrogen concentration of the nitrate in the effluent of the first anoxic reactor is higher than a set value C1And the holding time exceeds the set value T2When the second anoxic/aerobic reactor is in use, the aeration is closed and the stirring is started, and the aerobic state is changed into the anoxic state.
The fifth aerobic reactor carries out aeration regulation according to the following processes:
when the ammonia nitrogen concentration at the water outlet end of the fifth aerobic reactor is higher than or equal to the set value C2In the meantime, the aeration rate is increased until the oxygen water is dissolvedThe concentration reaches and is maintained at 6-8 mg/L; when the ammonia nitrogen concentration of the water outlet end of the fifth aerobic reactor is lower than or equal to a set value C3(C3＜C2) When the ammonia nitrogen concentration is higher than the set value C, the aeration quantity is gradually reduced until the ammonia nitrogen concentration of the effluent is higher than the set value C3And is lower than the set value C2Controlling the minimum aeration rate to be 10m3/(m2·h)。
A nitrifying liquid reflux pump is arranged between the fifth aerobic reactor and the first anoxic reactor, and the effluent nitrifying liquid of the fifth aerobic reactor is refluxed into the first anoxic reactor through a pipeline (channel). The total COD in the first anoxic reactor is obtained by monitoring the water inflow and the COD concentration of the inflow of the first anoxic reactor on line, and the total COD is calculated according to the set value theta of the carbon-nitrogen ratio (C/N)1Determining the total amount of nitrate nitrogen required to enter the first anoxic reactor, and further determining the reflux amount according to the nitrate nitrogen concentration of the effluent of the fifth aerobic reactor, wherein if the reflux ratio is more than 200%, the reflux ratio is 200%, and if the reflux ratio is less than 50%, the reflux ratio is 50%.
A carbon source adding device is arranged in the sixth anoxic reactor, the total amount of nitrate entering the sixth anoxic reactor is calculated according to the nitrogen concentration of nitrate in the effluent of the fifth aerobic reactor, and the total amount of nitrate enters the sixth anoxic reactor according to the set value theta of the carbon-nitrogen ratio (C/N)2And determining the adding amount of the carbon source.
Each reactor adopts a cylindrical or rectangular tank body, the diameter-depth ratio of the cylindrical tank body is 2: 1-0.5: 1, and the effective depth is 4-10 m; the length-width ratio of the rectangular tank body is 0.5: 1-1.5: 1, the effective depth is 4-10 m, and the maximum flow velocity of the overflowing section is not higher than 35 m/h.
Each reactor all is provided with into water distribution device and goes out water-collecting device, and the water distribution device of intaking adopts weir crest upper portion water distribution or submerged formula to be close to reactor side bottom water distribution, corresponds out water-collecting device and then close to reactor side bottom behind the interception screen cloth and catchment or be close to reactor side top and catchment, and each reactor business turn over water mode adopts the mode of going into from top to bottom or going into from top to bottom, and the emergence of reactor short-term flow phenomenon is avoided in control hydraulic flow state.
In the first-stage A/O unit, the first anoxic reactor is a preposed anoxic denitrification area, denitrification is carried out by utilizing an electron donor substrate provided by an organic carbon source in raw water to remove nitrate nitrogen, and effluent liquid of the fifth aerobic reactor carries the nitrate nitrogen to flow back to the first anoxic reactor in the reaction process; the second anoxic/aerobic reactor is used as an anoxic denitrification/aerobic organic matter degradation regulation area, utilizes an electron donor substrate provided by an organic matter carbon source in raw water to perform denitrification to remove nitrate nitrogen in an anoxic state, is used as a supplement of the first anoxic reactor to ensure that the preposed denitrification reaction is fully and thoroughly performed, and is used as an organic matter aerobic degradation area in an aerobic state to degrade and remove organic matters in sewage entering the reactor so as to ensure that a subsequent aerobic reaction area is in a low organic load state; when the second anoxic/aerobic reactor is in an anoxic state, the third aerobic reactor is used as an organic matter aerobic degradation zone to degrade and remove organic matters in the sewage entering the reactor so as to ensure that a subsequent aerobic reaction zone is in a low organic load state, and when the second anoxic/aerobic reactor is in an aerobic state, the third aerobic reactor is used as an aerobic organic matter degradation and nitration reaction zone to remove organic matters, organic nitrogen and ammonia nitrogen entering the reactor; the fourth aerobic reactor is used as an aerobic nitrification reaction zone to remove organic nitrogen and ammonia nitrogen entering the reactor; the fifth aerobic reactor is used as an aerobic nitrification reaction zone capable of adjusting aeration and controlling the dissolved oxygen level and is used as a supplement of the fourth reactor to ensure full and thorough nitrification reaction.
In the second-stage A/O unit, the sixth anoxic reactor and the seventh anoxic reactor are used as a post-denitrification area, the added exogenous carbon source is used as a denitrification electron donor substrate for denitrification to remove nitrate nitrogen, and the removal amount of the nitrate nitrogen is controlled by adjusting the adding amount of the exogenous carbon source according to the discharge target requirement of the total nitrogen of the finally treated effluent in the reaction process; the eighth aerobic reactor is used for degrading and removing organic matters remained in the effluent of the seventh anoxic reactor and is used as a supplement for the nitration reaction of the first-stage A/O unit so as to ensure that the final effluent is controlled according to the design requirement, and the organic matters, the total nitrogen, the ammonia nitrogen and the like meet the water quality index requirement.
The operation process of the system for treating sewage is as follows:
by adopting a continuous flow operation mode, pretreated sewage enters a first anoxic reactor, a second anoxic/aerobic reactor, a third aerobic reactor, a fourth aerobic reactor and a fifth aerobic reactor of a first-stage A/O unit in sequence through lifting, a sixth anoxic reactor, a seventh anoxic reactor and an eighth aerobic reactor of a second-stage A/O unit, and finally water is separated through muddy water clarification.
The invention has the following beneficial characteristics:
(1) aiming at the high discharge standard of urban sewage treatment, the invention realizes the effective control of the denitrification capability of the system according to the treatment target requirement by accurately controlling the addition of the exogenous carbon source in the post denitrification while improving the high utilization and denitrification efficiency of the carbon source in the raw water through the arrangement of pre-denitrification and post-denitrification, thereby achieving the most economical efficiency and stability of the sewage denitrification treatment;
(2) the reaction space and the operation condition can be automatically controlled and adjusted, and the economic operation of sewage treatment is realized through partial functional adjustment of the reactor and the control mode of dissolved oxygen under the condition of fluctuating water quality, water quantity and water temperature;
(3) the reactor series structure realizes the optimized distribution of the organic load and the ammonia nitrogen load on the space, and creates favorable conditions for the efficient removal of organic matters and the system nitration;
(4) the method has the advantages that activated sludge is replaced by a biological membrane, the concentration (SS) of suspended matters in effluent of the two-stage A/O reaction unit is only 50-200 mg/L, the microbial yield of the biological membrane and the sludge yield of a system are remarkably reduced, and the traditional secondary sedimentation tank and MBR membrane filtration technology adopted by an activated sludge method can be replaced by high-efficiency sludge-water clarification separation technologies such as an air flotation tank, a high-density sedimentation tank, magnetic flocculation separation, screen filtration and multi-medium filtration;
(5) the problems that the urban sewage is generally limited in low-temperature nitrification under the low-temperature condition in winter, the raw water is low in carbon-nitrogen ratio and cannot meet the requirement of biological denitrification and the like are solved;
(6) solves the problem that the existing A mainly takes the suspension growth activated sludge2The long theoretical hydraulic retention time and the high reflux ratio of the sludge and the nitrifying liquid required by the O process and the deformation process thereof cause large engineering investment and high operation energy consumptionAnd the like.
Drawings
FIG. 1 is a schematic diagram of a sewage treatment system with two-stage anoxic/aerobic combined reaction zone biological membrane.
In the figure: 1. the system comprises a first anoxic reactor, 2, a second anoxic/aerobic reactor, 3, a third aerobic reactor, 4, a fourth aerobic reactor, 5, a fifth aerobic reactor, 6, a sixth anoxic reactor, 7, a seventh anoxic reactor, 8, an eighth aerobic reactor, 9, a sludge-water clarification and separation unit, 10, a suspended biofilm carrier, 11, a stirring device, 12, an aeration device, 13, a suspended biofilm carrier interception screen, 14, a carbon source feeding device, 15, a nitrifying liquid reflux pump, 16, a controller, 17, 18, and 19.
Detailed Description
As shown in figure 1, the two-stage anoxic/aerobic biomembrane sewage treatment system with adjustable reaction zones comprises a first-stage A/O unit, a second-stage A/O unit and a sludge-water clarification and separation unit 9 which are sequentially connected.
The first-stage A/O unit comprises a first anoxic reactor 1, a second anoxic/aerobic reactor 2, a third aerobic reactor 3, a fourth aerobic reactor 4 and a fifth aerobic reactor 5 which are connected in sequence. The second-stage A/O unit comprises a sixth anoxic reactor 6, a seventh anoxic reactor 7 and an eighth aerobic reactor 8 which are connected in sequence. Each reactor (1-8) adopts a cylindrical or rectangular tank body, the diameter-depth ratio of the cylindrical tank body is 2: 1-0.5: 1, and the effective depth is 4-10 m; the length-width ratio of the rectangular tank body is 0.5: 1-1.5: 1, the effective depth is 4-10 m, and the maximum flow velocity of the overflowing section is not higher than 35 m/h.
Each reactor (1-8) is provided with a water inlet distribution device and a water outlet collection device, the water inlet distribution device adopts weir crest upper part water distribution or submerged water distribution close to the bottom of the side surface of the reactor, the corresponding water outlet collection device collects water close to the bottom of the side surface of the reactor or close to the top of the side surface of the reactor after intercepting a screen, the water inlet and outlet mode of each reactor adopts an upper inlet and lower outlet mode or a lower inlet and upper outlet mode, and the hydraulic flow state is controlled to avoid the short flow phenomenon of the reactor.
Suspended biofilm carriers 10 are filled in each reactor (1-8). Wherein, the filling rate in the first, sixth and seventh anoxic reactors (1, 2, 6 and 7) is not more than 45 percent, the filling rate in the second anoxic/aerobic reactor 2 and the fifth aerobic reactor 5 is not more than 40 percent, and the filling rate in the third, fourth and eighth aerobic reactors (3, 4 and 8) is not more than 55 percent.
Stirring devices 11 are arranged in the first, sixth and seventh anoxic reactors (1, 2 and 7) and the second anoxic/aerobic reactor 2. The stirring device 11 adopts a spiral or hyperboloid stirrer, and the stirring input power is not less than 25W/m3。
Aeration devices 12 are arranged in the third, fourth, fifth and eighth aerobic reactors (3, 4, 5 and 8) and the second anoxic/aerobic reactor 2. The aeration device 12 adopts a mode of arranging perforated pipes on one side for aeration, the perforated pipes are arranged at the bottom of the 2/3 pool close to one side of the water outlet, the aeration holes of the perforated pipes are arranged in a mode of close water outlet end encryption arrangement, the aperture of each aeration hole is 3-6 mm, and the ventilation volume of each aeration hole opening is 1.60-1.75 m3And h, the installation level error of the perforated pipe is not more than 6.5 mm.
Each reactor (1-8) is internally provided with an effluent suspended biofilm carrier interception screen 13, the maximum sieving flow speed of the interception screen is not more than 60m/h, the aperture ratio of the interception screen is not more than 60%, and the aperture of the screen is 60% of the diameter of the suspended biofilm carrier. The interception screen 13 can adopt a vertical or horizontal cylindrical screen; when the vertical screen is adopted, the opening surface of the screen is positioned at the position of 35 to 65 percent of the effective water depth of the tank body; when a horizontal transverse cylindrical screen is adopted, the installation height of the cylindrical screen is 35-65% of the effective water depth of the tank body.
The water inlet end of the system (the water inlet end of the first anoxic reactor 1) is provided with an online flow analyzer and an online COD analyzer for obtaining the water inlet flow and the COD concentration of the inlet water. The water outlet end of the first anoxic reactor 1 is provided with an online nitrate nitrogen analyzer to obtain the nitrate nitrogen concentration of the outlet water. The water outlet end of the fifth aerobic reactor 5 is provided with an online ammonia nitrogen analyzer, an online nitrate nitrogen analyzer and an online dissolved oxygen analyzer, and is used for obtaining the ammonia nitrogen concentration, the nitrate nitrogen concentration and the dissolved oxygen concentration of the effluent. These analyzers are prior art.
The second anoxic/aerobic reactor 2 has an adjustable function, and the stirring device and the aeration device in the reactor are controlled by the controller 16 to operate according to the following processes:
when the second anoxic/aerobic reactor 2 is in a state that the stirring device is opened and the aeration device is closed, the reactor 2 is used as an anoxic denitrification reactor for denitrification; when the nitrogen concentration of nitrate in the effluent of the first anoxic reactor 1 is lower than or equal to the set value C1And the holding time exceeds the set value T1When the second anoxic/aerobic reactor 2 is in use, the stirring device is automatically closed, the aeration device is opened, the anoxic state is converted into the aerobic state, and the reactor 2 is used as an aerobic reactor to degrade organic matters. When the nitrogen concentration of the nitrate in the effluent of the first anoxic reactor 1 is higher than the set value C1And the holding time exceeds a certain set value T2When the second anoxic/aerobic reactor 2 is in use, the aeration system is automatically closed and the stirring system is started, namely the aerobic state is converted into the anoxic state.
The fifth aerobic reactor 5 has an aeration adjusting function, controls a stirring device and an aeration device in the reactor through a controller 17, and operates according to the following processes:
when the ammonia nitrogen concentration at the water outlet end of the fifth aerobic reactor 5 is higher than or equal to the set value C2When the oxygen content is higher than the preset value, the aeration amount is increased until the dissolved oxygen level reaches and is maintained at 6-8 mg/L; when the ammonia nitrogen concentration of the water outlet end of the fifth aerobic reactor 5 is lower than or equal to the set value C3(C3＜C2) When the ammonia nitrogen concentration is higher than the set value C, the aeration quantity is gradually reduced until the ammonia nitrogen concentration of the effluent is higher than the set value C3And is lower than the set value C2Controlling the minimum aeration rate to be 10m3/(m2·h)。
Set value C1And a set value C2And a set value C3And a set value T1And a set value T2The determination needs to be specifically determined according to the final effluent ammonia nitrogen requirement and the final effluent total nitrogen requirement so as to meet the final effluent requirement for adjustment.
A nitrifying liquid reflux pump 15 is arranged between the fifth aerobic reactor 5 and the first anoxic reactor 1, the reflux pump 15 is connected with a controller 18, and the reflux pump 15 adopts a low-lift large-flow axial-flow pump. Reflux of nitrifying liquidThe controller 18 controls the reflux pump 15 to reflux the effluent nitrified liquid of the fifth aerobic reactor 5 to the first anoxic reactor 1 through a pipeline (canal). The total COD in the first anoxic reactor 1 is obtained by monitoring the water inflow and the COD concentration of the inflow water of the first anoxic reactor 1 on line, and the total COD is calculated according to the set value theta of the carbon-nitrogen ratio (C/N)1Determining the total amount of nitrate nitrogen required to enter the first anoxic reactor 1, and further determining the reflux amount according to the concentration of nitrate nitrogen in the effluent of the fifth aerobic reactor 5, wherein the reflux ratio is 200% if the reflux ratio is more than 200%, and 50% if the reflux ratio is less than 50%.
A carbon source adding device 14 is arranged in the sixth anoxic reactor 6, the carbon source adding device 14 is connected with a controller 19, and the controller 19 controls the adding amount of the carbon source adding device 14. Obtaining the total amount of nitrate entering the sixth anoxic reactor 6 according to the nitrogen concentration of nitrate in the effluent of the fifth aerobic reactor 5, and according to the set value theta of the carbon-nitrogen ratio (C/N)2And determining the adding amount of the carbon source.
Set value (theta) of carbon-nitrogen ratio (C/N)1And theta2) All can be determined empirically, theta1And theta2The prior art is concerned with the types of raw water and carbon source, respectively, each of which has empirical values.
In the first-stage A/O unit, the first anoxic reactor 1 is a preposed anoxic denitrification area, denitrification is carried out by utilizing an electron donor substrate provided by an organic carbon source in raw water to remove nitrate nitrogen, and in the reaction process, effluent of the fifth aerobic reactor 5 flows back to the first anoxic reactor 1 through a nitrifying liquid reflux pump 15. The second anoxic/aerobic reactor 2 is an anoxic denitrification/aerobic organic matter degradation regulation area, when the reactor 2 is in an anoxic state, the reactor utilizes an electron donor substrate provided by an organic matter carbon source in raw water to carry out denitrification to remove nitrate nitrogen, and the second anoxic/aerobic reactor is used as a supplement of the first anoxic reactor 1 to ensure that the preposed denitrification reaction is fully and thoroughly carried out; when the reactor 2 is in an aerobic state, the reactor is used as an organic matter aerobic degradation zone to degrade and remove organic matters in the sewage entering the reactor so as to ensure that a subsequent aerobic reaction zone is in a low organic load state; when the second anoxic/aerobic reactor 2 is in an anoxic state, the third aerobic reactor 3 is used as an organic matter aerobic degradation zone to degrade and remove organic matters in the sewage entering the reactor so as to ensure that a subsequent aerobic reaction zone is in a low organic load state, and when the second anoxic/aerobic reactor 2 is in an aerobic state, the third aerobic reactor 3 is used as an aerobic organic matter degradation and nitration reaction zone to remove organic matters, organic nitrogen and ammonia nitrogen entering the reactor; the fourth aerobic reactor 4 is used as an aerobic nitrification reaction zone to remove organic nitrogen and ammonia nitrogen entering the reactor. The fifth aerobic reactor 5 is used as an aerobic nitrification reaction zone which can adjust aeration and control the dissolved oxygen level and is used as a supplement of the fourth reactor 4 to ensure that the nitrification reaction is fully and thoroughly carried out.
In the second-stage A/O unit, the sixth anoxic reactor 6 and the seventh anoxic reactor 7 are used as a post-denitrification area, and an added exogenous carbon source is used as a denitrification electron donor substrate for denitrification to remove nitrate nitrogen. The eighth aerobic reactor 8 mainly degrades and removes residual organic matters in the effluent of the seventh anoxic reactor 7, and can also perform nitrification to supplement the nitrification reaction of the first-stage a/O unit (which can also be understood as the nitrification reaction of the second-stage a/O unit, but it is just supplementary, and is not mainly performing nitrification reaction) so as to ensure that the water quality indexes of organic matters, total nitrogen, ammonia nitrogen and the like in the final treated water are controlled according to the design requirements.
The sludge-water clarifying and separating unit 9, the carbon source adding device 14 and each controller adopt the prior art.
The system is adopted to treat primary effluent of an actual sewage treatment plant, and the specific implementation mode is completed according to the following steps:
(1) suspended biofilm carrier biofilm culturing
Respectively putting a certain amount of suspended biological carriers 10 into a third aerobic reactor, a fourth aerobic reactor, an eighth aerobic reactor (3, 4, 8) and a second anoxic/aerobic reactor 2, and controlling the adding filling rate of the reactors (2, 3, 4, 5, 8) to be 55%; adding raw water into the reactors to the normal reaction control liquid level of the reactors, starting the aeration devices 12 of the reactors to perform oxygenation aeration, and controlling aeration to supply airIntensity is not more than 55m3/(m2H), culturing and biofilm culturing are carried out on the dissolved oxygen at 4-5 mg/L, and the sewage in the reactor is updated once a day in the first 5 days; updating the sewage in the reactor twice every day in 5-10 days; and after 10 days, monitoring the main water quality indexes of COD and ammonia nitrogen for the mixed liquid of the reactor inlet water and different reaction periods, and simultaneously observing the biofilm formation state, wherein after the COD removal rate of the outlet water in each treatment period reaches about 80 percent and an effective biofilm formation is formed, the biofilm formation culture of the suspended biofilm carrier is completed.
(2) Initial start-up
Distributing the suspended biological membrane carrier 10 which finishes biofilm culturing into each reactor (1-8) according to the filling rate that the first, sixth and seventh anoxic reactors (1, 6 and 7) are not more than 45%, the second anoxic/aerobic reactor 2 and the fifth aerobic reactor 5 are not more than 40%, and the third, fourth and eighth aerobic reactors (3, 4 and 8) are not more than 55%.
And a continuous water inlet and outlet operation mode is adopted, and the water inlet flow is controlled to be 20-50% of the designed flow.
The stirring device 11 is started to lead the suspended biological film carriers 10 in the first, sixth and seventh anoxic reactors (1, 6 and 7) and the second anoxic/aerobic reactor 2 to be fully fluidized. The aeration device 12 is started to lead the suspended biological film carriers in the third, fourth and eighth aerobic reactors (3, 4 and 8) and the fifth aerobic reactor 5 to be fully fluidized. The reflux pump 15 is started to lift and reflux the effluent of the fifth aerobic reactor 5 to the first anoxic reactor 1 through the pipeline (canal), and the reflux ratio is controlled to be 100 percent.
Starting the carbon source adding device 14 and the controller 19, for example, using sodium acetate as an external carbon source, and setting theta1The carbon source amount is automatically controlled to be 4.0: 1. Meanwhile, paying attention to COD, ammonia nitrogen and nitrate nitrogen of system inlet water and outlet water of the eighth reactor, observing the biofilm formation state, gradually increasing the system inlet water flow and load after the removal rate of the COD, ammonia nitrogen and total nitrogen of the final outlet water to be treated reaches about 80%, and forming an effective biofilm formation until the system treatment load reaches the specified treatment load condition.
(3) Formal operation
After the predetermined processing load condition is reached, the whole system is optimally controlled.
Adjusting the stirring intensity of the first, sixth and seventh anoxic reactors (1, 6 and 7) and the second anoxic/aerobic reactor 2, and reducing the stirring intensity as much as possible on the premise of ensuring the full fluidization of the suspended biological membrane carrier; and adjusting the aeration intensity of the third, fourth, fifth and eighth reactors (3, 4, 5 and 8), and controlling the dissolved oxygen level to be 5-7 mg/L on the premise of ensuring the full fluidization of the suspended biomembrane carrier.
Starting the nitrifying liquid reflux controller 18 according to theta2The set value is 6.5:1 to control the reflux amount; keeping the carbon source adding device 14 and the controller 19 in an opening state according to theta1The setting value is 4.0:1 to control the adding amount of the carbon source.
The water quality of inlet and outlet water of the embodiment is as follows: under the condition of reaction temperature of 8-25 ℃, the COD concentration of inlet water ranges from 76-284 mg/L, and the average outlet water concentration is 29.3 +/-10.6 mg/L; the concentration range of the ammonia nitrogen of the inlet water is 21.8-85.1 mg/L, and the concentration of the ammonia nitrogen of the outlet water is 0.14 +/-0.33 mg/L; the total nitrogen concentration range of inlet water is 25.7-87.8 mg/L, and the average outlet water concentration is 2.7 +/-3.4 mg/L. Under the condition of fluctuating reaction conditions, the system achieves stable pollutant removal effect.
Claims (5)
1. A reaction partition adjustable two-stage anoxic/aerobic biomembrane sewage treatment system is characterized in that: the device comprises a first-stage A/O unit and a second-stage A/O unit which are connected in sequence; the first-stage A/O unit comprises a first anoxic reactor, a second anoxic/aerobic reactor, a third aerobic reactor, a fourth aerobic reactor and a fifth aerobic reactor which are connected in sequence; the second-stage A/O unit comprises a sixth anoxic reactor, a seventh anoxic reactor and an eighth aerobic reactor which are connected in sequence; suspended biological membrane carriers are filled in each reactor; stirring devices are arranged in the first anoxic reactor, the sixth anoxic reactor and the seventh anoxic reactor and in the second anoxic/aerobic reactor; aeration devices are arranged in the third aerobic reactor, the fourth aerobic reactor, the fifth aerobic reactor, the eighth aerobic reactor and the second anoxic/aerobic reactor;
the second anoxic/aerobic reactor is controlled and regulated according to the following processes:
when the second anoxic/aerobic reactor is in a state of stirring opening and aeration closing, the second anoxic/aerobic reactor is used as an anoxic denitrification reactor for denitrification; when the nitrogen concentration of nitrate in the effluent of the first anoxic reactor is lower than or equal to the set value C1And the holding time exceeds the set value T1When the second anoxic/aerobic reactor is used, the stirring is automatically closed, the aeration is started, namely the anoxic state is converted into the aerobic state, and the reactor is used as an aerobic reactor for organic matter degradation; when the nitrogen concentration of the nitrate in the effluent of the first anoxic reactor is higher than a set value C1And the holding time exceeds the set value T2When the anaerobic reaction is finished, the aeration of the second anoxic/aerobic reactor is closed and the stirring is started, and the aerobic state is converted into the anoxic state;
a nitrifying liquid reflux pump is arranged between the fifth aerobic reactor and the first anoxic reactor, and nitrifying liquid flowing out of the fifth aerobic reactor flows back to the first anoxic reactor; the total COD in the first anoxic reactor is obtained by monitoring the water inflow and the COD concentration of the inflow of the first anoxic reactor on line, and the total COD is calculated according to the set value theta of the carbon-nitrogen ratio1Determining the total amount of nitrate nitrogen required to enter the first anoxic reactor, and further determining according to the nitrate nitrogen concentration of the effluent of the fifth aerobic reactorThe reflux ratio in this case was 200% when the reflux ratio was more than 200%, and 50% when the reflux ratio was less than 50%.
2. The two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones of claim 1, which is characterized in that: the filling rate of the suspended biological membrane carrier is as follows: the filling rate in the first anoxic reactor, the sixth anoxic reactor and the seventh anoxic reactor is not more than 45 percent, the filling rate in the second anoxic/aerobic reactor and the fifth aerobic reactor is not more than 40 percent, and the filling rate in the third aerobic reactor, the fourth aerobic reactor and the eighth aerobic reactor is not more than 55 percent.
3. The two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones of claim 1, which is characterized in that: the water inlet end of the first-stage A/O unit is provided with an online flow analyzer and an online COD analyzer; the water outlet end of the first anoxic reactor is provided with an online nitrate nitrogen analyzer; and the water outlet end of the fifth aerobic reactor is provided with an online ammonia nitrogen analyzer, an online nitrate nitrogen analyzer and an online dissolved oxygen analyzer.
4. The two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones of claim 1, which is characterized in that: the fifth aerobic reactor carries out aeration regulation according to the following processes:
when the ammonia nitrogen concentration at the water outlet end of the fifth aerobic reactor is higher than or equal to the set value C2When the oxygen content is higher than the preset value, the aeration amount is increased until the dissolved oxygen level reaches and is maintained at 6-8 mg/L; when the ammonia nitrogen concentration of the water outlet end of the fifth aerobic reactor is lower than or equal to a set value C3When, C3＜C2Gradually reducing the aeration rate until the ammonia nitrogen concentration of the effluent is higher than a set value C3And is lower than the set value C2Controlling the minimum aeration rate to be 10m3/(m2·h)。
5. The two-stage anoxic/aerobic biofilm sewage treatment system with adjustable reaction zones as claimed in claim 1, wherein the two-stage anoxic/aerobic biofilm sewage treatment system is characterized in that: a carbon source adding device is arranged in the sixth anoxic reactor, the total amount of nitrate entering the sixth anoxic reactor is calculated according to the nitrogen concentration of nitrate in the effluent of the fifth aerobic reactor, and the total amount of nitrate enters the sixth anoxic reactor according to the set value theta of the carbon-nitrogen ratio2And determining the adding amount of the carbon source.
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| CN111533258B (en) | 2020-05-07 | 2022-01-28 | 青岛理工大学 | Low-temperature segmented water-feeding multi-stage anoxic/aerobic sewage biological denitrification treatment method |
| CN111533259B (en) * | 2020-05-07 | 2021-09-03 | 青岛理工大学 | Reaction partition adjustable two-stage anoxic/aerobic biological membrane sewage treatment system |
| CN114314824B (en) * | 2021-12-15 | 2023-11-03 | 深圳市益嘉昇科技有限公司 | Device and method for treating denitrification and anoxic wastewater |
| CN114735820A (en) * | 2022-03-09 | 2022-07-12 | 安徽中环环保科技股份有限公司 | Multistage A/O (anoxic/oxic) series batch water inlet type low-carbon source sewage denitrification device and method |
| CN114604967B (en) * | 2022-03-11 | 2023-06-23 | 青岛思普润水处理股份有限公司 | MBBR (moving bed biofilm reactor) reinforced AOA (automated optical inspection) and AAO (anaerobic-anoxic-oxic) dual-mode operation method based on circulating flow |
| CN114604966B (en) * | 2022-03-11 | 2023-07-21 | 青岛思普润水处理股份有限公司 | Micro-power-based MBBR enhanced AOA and AAO dual-mode system and operation method |
| CN114890545A (en) * | 2022-04-24 | 2022-08-12 | 陕西锦科环保工程有限公司 | Low-temperature sewage denitrification treatment system and method |
| CN115159681A (en) * | 2022-07-29 | 2022-10-11 | 江苏河马井股份有限公司 | Multistage good anaerobism sewage treatment system |
| CN115215438B (en) * | 2022-08-03 | 2024-05-03 | 中持水务股份有限公司 | Precise aeration and dosing combined control method and system for multi-stage AO biochemical pool |
| CN115818825A (en) * | 2022-10-19 | 2023-03-21 | 青岛理工大学 | Integrated efficient biological membrane reaction system suitable for rural domestic sewage treatment |
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